HRP20191157T1 - Multistage resid hydrocracking - Google Patents

Multistage resid hydrocracking Download PDF

Info

Publication number
HRP20191157T1
HRP20191157T1 HRP20191157TT HRP20191157T HRP20191157T1 HR P20191157 T1 HRP20191157 T1 HR P20191157T1 HR P20191157T T HRP20191157T T HR P20191157TT HR P20191157 T HRP20191157 T HR P20191157T HR P20191157 T1 HRP20191157 T1 HR P20191157T1
Authority
HR
Croatia
Prior art keywords
fraction
residue
stage
reactor
effluent
Prior art date
Application number
HRP20191157TT
Other languages
Croatian (hr)
Inventor
Mario C. Baldassari
Ujjal K. Mukherjee
Avinash Gupta
Original Assignee
Lummus Technology Llc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Lummus Technology Llc filed Critical Lummus Technology Llc
Publication of HRP20191157T1 publication Critical patent/HRP20191157T1/en

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • C10G67/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including solvent extraction as the refining step in the absence of hydrogen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • C10G67/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including solvent extraction as the refining step in the absence of hydrogen
    • C10G67/0454—Solvent desasphalting
    • C10G67/049—The hydrotreatment being a hydrocracking
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/003—Solvent de-asphalting
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/107—Atmospheric residues having a boiling point of at least about 538 °C
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1077—Vacuum residues
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/202—Heteroatoms content, i.e. S, N, O, P
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/205—Metal content
    • C10G2300/206—Asphaltenes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/30—Physical properties of feedstocks or products
    • C10G2300/301—Boiling range
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/42—Hydrogen of special source or of special composition

Claims (15)

1. Postupak za poboljšanje ostatka, naznačen time, da sadržava: hidrokrekiranje ostatka u prvom reakcijskom stupnju (14) da bi se dobio efluent prvog stupnja; hidrokrekiranje deasfaltirane uljne frakcije u drugom reakcijskom stupnju (22) da bi se dobio efluent drugog stupnja; dovođenje efluenta iz prvog stupnja i iz drugog stupnja u sustav za odvajanje (26); frakcioniranje efluenta iz prvog stupnja i efluenta iz drugog stupnja u sustavu za odvajanje (26) da bi dobila najmanje jedna ugljikovodična frakcija destilata i frakcije ugljikovodičnog ostatka; te dovođenje ugljične frakcije ostatka u jedinicu za deasfaltiranje otapalom (32) kako bi se dobila asfaltenska frakcija i deasfaltirana uljna frakcija, pri čemu hidrokrekiranje ostatka obuhvaća: dovođenje vodika i ostatka u prvi reaktor koji sadržava prvi katalizator za hidrokrekiranje; dovođenje u kontakt ostatka i vodika u prisutnosti prvog katalizatora za hidrokrekiranje pod određenim uvjetima temperature i tlaka da bi se razbio barem dio ostatka; vraćanje efluenta iz prvog stupnja iz prvog reaktora; pri čemu hidrokrekiranje deasfaltirane uljne frakcije obuhvaća: dovođenje vodika i deasfaltirane uljne frakcije u drugi reaktor koji sadržava drugi katalizator za hidrokrekiranje; dovođenje deasfaltirane uljne frakcije i vodika u prisutnosti drugog katalizatora za hidrokrekiranje pod određenim uvjetima temperature i tlaka da bi se razbio barem dio deasfaltiranog ulja; te obnavljanje efluenta iz drugog stupnja iz drugog reaktora, i pri čemu frakcioniranje obuhvaća: razdvajanje efluenta prvog i drugog stupnja u visokotlačnom visokotemperaturnom separatoru (40) radi dobivanja proizvoda plinovite faze i proizvoda tekuće faze; odvajanje proizvoda tekuće faze u atmosferskom destilacijskom tornju (54) kako bi se dobila frakcija koja sadržava ugljikovodike koji vriju u nizu atmosferskih destilata i prvu frakciju s dna koja sadržava ugljikovodike s uobičajenim vrelištem od najmanje 340 °C; odvajanje frakcije dna u vakuumskoj destilacijskoj koloni (60) da bi se dobila frakcija koja sadržava ugljikovodike s vrelištem u nizu vakuumskih destilata i drugu frakciju s dna koja sadržava ugljikovodike kojima je temperatura vrenja najmanje 480 °C; i dovođenje druge frakcije s dna u jedinicu za deasfaltiranje otapalom (32) kao ostatak ugljikovodične frakcije.1. A process for improving the residue, characterized in that it contains: hydrocracking the residue in the first reaction stage (14) to obtain the effluent of the first stage; hydrocracking the deasphalted oil fraction in the second reaction stage (22) to obtain the effluent of the second stage; bringing effluent from the first stage and from the second stage into the separation system (26); fractionating the effluent from the first stage and the effluent from the second stage in the separation system (26) to obtain at least one hydrocarbon fraction of the distillate and the hydrocarbon residue fraction; and feeding the carbon fraction of the residue to the solvent deasphalting unit (32) to obtain the asphaltene fraction and the deasphalted oil fraction, wherein the hydrocracking of the residue includes: feeding hydrogen and residue to the first reactor containing the first hydrocracking catalyst; contacting the residue with hydrogen in the presence of a first hydrocracking catalyst under certain conditions of temperature and pressure to crack at least a portion of the residue; return of effluent from the first stage from the first reactor; whereby the hydrocracking of the deasphalted oil fraction includes: feeding hydrogen and the deasphalted oil fraction to a second reactor containing a second hydrocracking catalyst; feeding the deasphalted oil fraction and hydrogen in the presence of a second hydrocracking catalyst under certain conditions of temperature and pressure to crack at least a portion of the deasphalted oil; and recovery of effluent from the second stage from the second reactor, i whereby fractionation includes: separation of the effluent of the first and second stage in a high-pressure, high-temperature separator (40) in order to obtain a product of the gaseous phase and a product of the liquid phase; separating the liquid phase product in an atmospheric distillation tower (54) to obtain a fraction containing hydrocarbons boiling in a series of atmospheric distillates and a first fraction from the bottom containing hydrocarbons with a normal boiling point of at least 340 °C; separating the bottom fraction in a vacuum distillation column (60) to obtain a fraction containing hydrocarbons with a boiling point in a series of vacuum distillates and another fraction from the bottom containing hydrocarbons boiling at least 480 °C; and feeding the second fraction from the bottom to the solvent deasphalting unit (32) as the rest of the hydrocarbon fraction. 2. Postupak u skladu s patentnim zahtjevom 1, naznačen time, da su najmanje jedna radna temperatura i radni tlak u drugom reakcijskom stupnju (22) veći od radne temperature i radnog tlaka prvog reakcijskog stupnja (14).2. The method according to patent claim 1, characterized in that at least one working temperature and working pressure in the second reaction stage (22) are higher than the working temperature and working pressure of the first reaction stage (14). 3. Postupak u skladu s patentnim zahtjevom 1, naznačen time, da se barem dio asfaltena u ostatku hidrokrekira u prvom reakcijskom stupnju (14).3. The method according to patent claim 1, characterized in that at least part of the asphaltene in the residue is hydrocracked in the first reaction stage (14). 4. Postupak u skladu s patentnim zahtjevom 1, naznačen time, da nadalje obuhvaća djelovanje prvog reakcijskog stupnja (14) na temperaturi i tlaku za hidrokrekiranje ostatka pri konverziji od oko 30 % težinskog udjela do oko 75 % težinskog udjela ostatka.4. The method according to patent claim 1, characterized in that it further comprises the operation of the first reaction stage (14) at temperature and pressure for hydrocracking the residue at conversion of about 30% by weight to about 75% by weight of the residue. 5. Postupak u skladu s patentnim zahtjevom 1, naznačen time, da nadalje obuhvaća djelovanje prvog reakcijskog stupnja (14) na temperaturi i tlaku za hidrokrekiranje ostatka uz ukupnu konverziju ostatka od najmanje 60 % težinskog udjela.5. The process according to patent claim 1, characterized in that it further comprises the operation of the first reaction stage (14) at temperature and pressure for hydrocracking the residue with a total conversion of the residue of at least 60% by weight. 6. Postupak u skladu s patentnim zahtjevom 5, naznačen time, da je ukupna konverzija ostatka najmanje 95 % težinskog udjela.6. The process according to claim 5, characterized in that the total conversion of the residue is at least 95% by weight. 7. Postupak u skladu s patentnim zahtjevom 1, naznačen time, da ostatak ugljikovodične frakcije sadržava ugljikovodike s uobičajenim vrelištem od najmanje 340 °C.7. Process according to claim 1, characterized in that the rest of the hydrocarbon fraction contains hydrocarbons with a normal boiling point of at least 340 °C. 8. Postupak u skladu s patentnim zahtjevom 1, naznačen time, da prvi reakcijski stupanj (14) obuhvaća reaktor s jednim vrijućim slojem.8. The method according to claim 1, characterized in that the first reaction stage (14) comprises a reactor with one fluidized bed. 9. Postupak u skladu s patentnim zahtjevom 1, naznačen time, da drugi reakcijski stupanj (22) obuhvaća najmanje jedan od reaktora s vrijućim slojem i reaktora s fiksnim slojem.9. The method according to claim 1, characterized in that the second reaction stage (22) comprises at least one of the fluidized bed reactor and the fixed bed reactor. 10. Postupak u skladu s patentnim zahtjevom 1, naznačen time, da nadalje obuhvaća hlađenje proizvoda plinovite faze radi dobivanja plinovite frakcije koja sadržava vodik i frakcije destilata; i dovođenje frakcije destilata u separaciju proizvoda tekuće faze.10. The method according to patent claim 1, characterized in that it further comprises cooling the gaseous phase product in order to obtain a gaseous fraction containing hydrogen and distillate fractions; and bringing the distillate fraction to the liquid phase product separation. 11. Postupak u skladu s patentnim zahtjevom 10, naznačen time, da nadalje obuhvaća recikliranje barem dijela obnovljenog vodika u barem jednom od prvog reaktora i drugog reaktora.11. The method according to claim 10, further comprising recycling at least part of the recovered hydrogen in at least one of the first reactor and the second reactor. 12. Postupak u skladu s patentnim zahtjevom 1, naznačen time, da nadalje obuhvaća hlađenje druge frakcije s dna izravnom izmjenom topline s najmanje jednim dijelom ostatka i dijelom prve frakcije s dna.12. The method according to claim 1, characterized in that it further comprises cooling the second fraction from the bottom by direct heat exchange with at least one part of the residue and part of the first fraction from the bottom. 13. Postupak u skladu s patentnim zahtjevom 1, naznačen time, da su barem radna temperatura ili radni tlak u drugom reaktoru manji od radne temperature i radnog tlaka prvog reaktora.13. The method according to claim 1, characterized in that at least the operating temperature or operating pressure in the second reactor is lower than the operating temperature and operating pressure of the first reactor. 14. Postupak u skladu s patentnim zahtjevom 1, naznačen time, da ostatak ugljikovodične frakcije sadržava ugljikovodike s uobičajenim vrelištem od najmanje 480 °C.14. The process according to patent claim 1, characterized in that the rest of the hydrocarbon fraction contains hydrocarbons with a normal boiling point of at least 480 °C. 15. Postupak u skladu s patentnim zahtjevom 1, naznačen time, da frakcioniranje obuhvaća dovođenje efluenta iz prvog stupnja i efluenta iz drugog stupnja u zajednički sustav za frakcioniranje.15. The method according to patent claim 1, characterized in that the fractionation comprises bringing the effluent from the first stage and the effluent from the second stage into a common system for fractionation.
HRP20191157TT 2009-06-23 2019-06-27 Multistage resid hydrocracking HRP20191157T1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
US12/490,089 US8287720B2 (en) 2009-06-23 2009-06-23 Multistage resid hydrocracking
EP10726674.4A EP2445993B1 (en) 2009-06-23 2010-06-16 Multistage resid hydrocracking
PCT/US2010/001736 WO2010151300A1 (en) 2009-06-23 2010-06-16 Multistage resid hydrocracking

Publications (1)

Publication Number Publication Date
HRP20191157T1 true HRP20191157T1 (en) 2019-10-18

Family

ID=42727438

Family Applications (2)

Application Number Title Priority Date Filing Date
HRP20191157TT HRP20191157T1 (en) 2009-06-23 2019-06-27 Multistage resid hydrocracking
HRP20210490TT HRP20210490T1 (en) 2009-06-23 2021-03-26 Multistage resid hydrocracking

Family Applications After (1)

Application Number Title Priority Date Filing Date
HRP20210490TT HRP20210490T1 (en) 2009-06-23 2021-03-26 Multistage resid hydrocracking

Country Status (17)

Country Link
US (3) US8287720B2 (en)
EP (2) EP2445993B1 (en)
KR (2) KR101696017B1 (en)
CN (2) CN102803441B (en)
BR (1) BRPI1015117B1 (en)
CA (1) CA2764971C (en)
EC (1) ECSP12011619A (en)
ES (2) ES2732813T3 (en)
HR (2) HRP20191157T1 (en)
HU (2) HUE053691T2 (en)
MX (1) MX2011013604A (en)
MY (3) MY194683A (en)
PL (2) PL2562235T3 (en)
PT (2) PT2562235T (en)
RU (2) RU2538961C1 (en)
SG (1) SG177364A1 (en)
WO (1) WO2010151300A1 (en)

Families Citing this family (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8287720B2 (en) 2009-06-23 2012-10-16 Lummus Technology Inc. Multistage resid hydrocracking
US10400184B2 (en) * 2011-08-31 2019-09-03 Exxonmobil Research And Engineering Company Hydroprocessing of heavy hydrocarbon feeds using small pore catalysts
US9028674B2 (en) 2013-01-17 2015-05-12 Lummus Technology Inc. Conversion of asphaltenic pitch within an ebullated bed residuum hydrocracking process
US20140221709A1 (en) * 2013-02-04 2014-08-07 Lummus Technology Inc. Integration of residue hydrocracking and solvent deasphalting
US20140221713A1 (en) * 2013-02-04 2014-08-07 Lummus Technology Inc. Residue hydrocracking processing
US9650312B2 (en) 2013-03-14 2017-05-16 Lummus Technology Inc. Integration of residue hydrocracking and hydrotreating
US10208261B2 (en) * 2014-02-12 2019-02-19 Lummus Technology Inc. Processing vacuum residuum and vacuum gas oil in ebullated bed reactor systems
RU2546677C1 (en) * 2014-03-27 2015-04-10 Игорь Анатольевич Мнушкин Method and installation of hydrocracking with obtaining motor fuels
US9663732B2 (en) 2014-09-09 2017-05-30 Uop Llc Process for controlling operations of a residue process unit
US9783748B2 (en) 2014-09-09 2017-10-10 Uop Llc Process for producing diesel fuel
EP3204473B1 (en) 2014-10-07 2020-05-06 Shell International Research Maatschappij B.V. A hydrocracking process integrated with solvent deasphalting to reduce heavy polycyclic aromatic buildup in heavy oil hydrocracker recycle stream
WO2016064776A1 (en) 2014-10-22 2016-04-28 Shell Oil Company A hydrocracking process integrated with vacuum distillation and solvent dewaxing to reduce heavy polycyclic aromatic buildup
US9695369B2 (en) 2014-11-21 2017-07-04 Lummus Technology Inc. Process to upgrade partially converted vacuum residua
US10144884B2 (en) 2015-06-18 2018-12-04 Uop Llc Two stage hydrocracking process and apparatus
US11015132B2 (en) * 2016-08-18 2021-05-25 Haldor Topsøe A/S High conversion hydrocracking process
WO2018119249A1 (en) * 2016-12-22 2018-06-28 Lummus Technology Inc. Multistage resid hydrocracking
US11788017B2 (en) 2017-02-12 2023-10-17 Magëmã Technology LLC Multi-stage process and device for reducing environmental contaminants in heavy marine fuel oil
US20190233741A1 (en) 2017-02-12 2019-08-01 Magēmā Technology, LLC Multi-Stage Process and Device for Reducing Environmental Contaminates in Heavy Marine Fuel Oil
US10604709B2 (en) 2017-02-12 2020-03-31 Magēmā Technology LLC Multi-stage device and process for production of a low sulfur heavy marine fuel oil from distressed heavy fuel oil materials
FR3075809B1 (en) 2017-12-21 2020-09-11 Ifp Energies Now PROCESS FOR CONVERTING HEAVY LOADS OF HYDROCARBONS WITH RECYCLE OF A DESASPHALTED OIL
US11261387B2 (en) * 2019-07-23 2022-03-01 Saudi Arabian Oil Company Fuel oil conversion
FR3113062B1 (en) 2020-07-30 2023-11-03 Ifp Energies Now Residue hydroconversion process with several hydroconversion stages integrating a deasphalting step

Family Cites Families (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NL7510465A (en) * 1975-09-05 1977-03-08 Shell Int Research PROCESS FOR CONVERTING HYDROCARBONS.
NL7612960A (en) 1976-11-22 1978-05-24 Shell Int Research METHOD FOR CONVERTING HYDROCARBONS.
US4176048A (en) 1978-10-31 1979-11-27 Standard Oil Company (Indiana) Process for conversion of heavy hydrocarbons
US4239616A (en) 1979-07-23 1980-12-16 Kerr-Mcgee Refining Corporation Solvent deasphalting
US4354928A (en) 1980-06-09 1982-10-19 Mobil Oil Corporation Supercritical selective extraction of hydrocarbons from asphaltic petroleum oils
US4354922A (en) 1981-03-31 1982-10-19 Mobil Oil Corporation Processing of heavy hydrocarbon oils
FR2504934A1 (en) 1981-04-30 1982-11-05 Inst Francais Du Petrole IMPROVED METHOD FOR SOLVENT DESASPHALTING OF HEAVY FRACTIONS OF HYDROCARBONS
US4536283A (en) 1984-08-20 1985-08-20 Exxon Research And Engineering Co. Integrated process for deasphalting heavy oils using a gaseous antisolvent
CA1222471A (en) 1985-06-28 1987-06-02 H. John Woods Process for improving the yield of distillables in hydrogen donor diluent cracking
GB8828335D0 (en) * 1988-12-05 1989-01-05 Shell Int Research Process for conversion of heavy hydrocarbonaceous feedstock
CA2010774A1 (en) 1989-06-12 1990-12-12 William L. Lafferty, Jr. Conversion increase of vacuum residiums
MX9502237A (en) * 1994-05-19 1997-02-28 Shell Int Research Process for conversion of a hydrocarbon residual oil.
FR2753982B1 (en) 1996-10-02 1999-05-28 Inst Francais Du Petrole MULTI-STAGE CATALYTIC PROCESS FOR CONVERTING A HEAVY HYDROCARBON FRACTION
US6514403B1 (en) * 2000-04-20 2003-02-04 Abb Lummus Global Inc. Hydrocracking of vacuum gas and other oils using a cocurrent/countercurrent reaction system and a post-treatment reactive distillation system
US6436279B1 (en) * 2000-11-08 2002-08-20 Axens North America, Inc. Simplified ebullated-bed process with enhanced reactor kinetics
US7214308B2 (en) 2003-02-21 2007-05-08 Institut Francais Du Petrole Effective integration of solvent deasphalting and ebullated-bed processing
US7279090B2 (en) 2004-12-06 2007-10-09 Institut Francais Du Pe'trole Integrated SDA and ebullated-bed process
ITMI20042445A1 (en) * 2004-12-22 2005-03-22 Eni Spa PROCEDURE FOR THE CONVERSION OF HEAVY CHARGES WHICH WEIGHING AND DISTILLATION WASTE
US7594990B2 (en) * 2005-11-14 2009-09-29 The Boc Group, Inc. Hydrogen donor solvent production and use in resid hydrocracking processes
CN100366709C (en) * 2006-04-17 2008-02-06 中国石油化工集团公司 Combined process for processing heavy oil
CN100569925C (en) * 2006-06-16 2009-12-16 中国石油化工股份有限公司 A kind of heavy, residual oil combinational processing method
ITMI20061512A1 (en) 2006-07-31 2008-02-01 Eni Spa PROCEDURE FOR THE TOTAL CONVERSION OF HEAVY DUTIES TO DISTILLATES
FR2906813A1 (en) 2006-10-06 2008-04-11 Inst Francais Du Petrole Heavy petroleum feed e.g. vacuum residue, hydroconverting method for producing petrol, involves de-asphalting vacuum residue to obtain de-asphalted oil, and recycling totality of oil by hydroconversion
US8287720B2 (en) 2009-06-23 2012-10-16 Lummus Technology Inc. Multistage resid hydrocracking

Also Published As

Publication number Publication date
CA2764971A1 (en) 2010-12-29
EP2445993B1 (en) 2019-03-27
KR20130114273A (en) 2013-10-16
PL2562235T3 (en) 2021-06-28
PT2562235T (en) 2021-03-22
MX2011013604A (en) 2012-02-21
RU2495911C2 (en) 2013-10-20
HRP20210490T1 (en) 2021-05-14
KR20120036989A (en) 2012-04-18
HUE053691T2 (en) 2021-07-28
US20100320122A1 (en) 2010-12-23
US9873839B2 (en) 2018-01-23
CN105838416A (en) 2016-08-10
KR101351147B1 (en) 2014-01-14
CA2764971C (en) 2014-05-06
WO2010151300A1 (en) 2010-12-29
ECSP12011619A (en) 2012-02-29
ES2856200T3 (en) 2021-09-27
US20160340597A1 (en) 2016-11-24
EP2562235B1 (en) 2020-12-30
BRPI1015117B1 (en) 2018-04-17
RU2013131001A (en) 2015-01-10
CN102803441B (en) 2016-05-11
US9441174B2 (en) 2016-09-13
RU2538961C1 (en) 2015-01-10
RU2012102048A (en) 2013-07-27
MY169463A (en) 2019-04-12
KR101696017B1 (en) 2017-01-13
US8287720B2 (en) 2012-10-16
CN105838416B (en) 2018-12-28
CN102803441A (en) 2012-11-28
BRPI1015117A2 (en) 2016-04-12
EP2445993A1 (en) 2012-05-02
EP2562235A1 (en) 2013-02-27
MY194683A (en) 2022-12-15
HUE044287T2 (en) 2019-10-28
PL2445993T3 (en) 2019-10-31
SG177364A1 (en) 2012-02-28
MY159468A (en) 2017-01-13
PT2445993T (en) 2019-07-10
US20120241357A1 (en) 2012-09-27
ES2732813T3 (en) 2019-11-26

Similar Documents

Publication Publication Date Title
HRP20191157T1 (en) Multistage resid hydrocracking
US9580663B2 (en) Process for hydrocracking a hydrocarbon feedstock
HRP20200493T1 (en) Integration of residue hydrocracking and hydrotreating
HRP20191938T1 (en) Conversion of asphaltenic pitch within an ebullated bed residuum hydrocracking process
US10760015B2 (en) Installation and integrated hydrotreatment and hydroconversion process with common fractionation section
CN107532089B (en) Process and apparatus for recovering hydroprocessed hydrocarbons using two strippers
RU2015137707A (en) Combining Hydrocracking and Deasphalting with a Cube Residue Solvent
FI2880132T3 (en) Residue hydrocracking
US9803148B2 (en) Hydrocracking process with interstage steam stripping
JP2009046657A (en) Method for producing raw material for preparing high-grade lubricating base oil from unconverted oil
KR20120101010A (en) Methods for producing hydrocarbon products from bio-oils and/or coal-oils
RU2015137682A (en) PROCESSING BY HYDROCRACKING OF CUBE REMAINING
EA036182B1 (en) Process and apparatus for hydroprocessing with two product fractionators
RU2015143892A (en) HYDRAULIC PROCESSING OF THERMAL CRACKING PRODUCTS
JP2014527100A5 (en)
EP2714851B1 (en) Multi-stage hydrocracking process for the hydroconversion of hydrocarbonaceous feedstocks
CN106906002B (en) Hydroprocessing or hydroconversion process using stripper and low pressure separator drum in fractionation section
US10815436B2 (en) Coil-wound heat exchanger for hydrotreatment or hydroconversion
EP3207106B1 (en) Methods and apparatus for recovery of hydrocarbons from fluid catalytic cracking slurry
EP2930225B1 (en) Process for hydrocracking a hydrocarbon feedstock
CN106350111B (en) A kind of coal tar deep processing method based on hydrofining reaction, modification reaction
EP2630218B1 (en) Process for hydrocracking a hydrocarbon feedstock
US20120312721A1 (en) Predicting petroleum coke morphology from feedstock properties